EP0003853B1 - Verfahren zur kontinuierlichen Konvertierung von NE-Metallsulfidkonzentraten - Google Patents

Verfahren zur kontinuierlichen Konvertierung von NE-Metallsulfidkonzentraten Download PDF

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Publication number
EP0003853B1
EP0003853B1 EP79200059A EP79200059A EP0003853B1 EP 0003853 B1 EP0003853 B1 EP 0003853B1 EP 79200059 A EP79200059 A EP 79200059A EP 79200059 A EP79200059 A EP 79200059A EP 0003853 B1 EP0003853 B1 EP 0003853B1
Authority
EP
European Patent Office
Prior art keywords
reactor
oxygen
ferrous metal
lead
phase
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP79200059A
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German (de)
English (en)
French (fr)
Other versions
EP0003853A1 (de
Inventor
Werner Dr. Schwartz
Peter Dr. Fischer
Heinrich Dr. Traulsen
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
GEA Group AG
Original Assignee
Metallgesellschaft AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Metallgesellschaft AG filed Critical Metallgesellschaft AG
Publication of EP0003853A1 publication Critical patent/EP0003853A1/de
Application granted granted Critical
Publication of EP0003853B1 publication Critical patent/EP0003853B1/de
Expired legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/12—Dry methods smelting of sulfides or formation of mattes by gases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the invention relates to a process for the continuous conversion of non-ferrous metal sulfide concentrates into a liquid non-ferrous metal-rich phase and a slag phase in an elongated, lying reactor, under a gas atmosphere containing zones of SO Z , sulfidic concentrates of copper, nickel, antimony, cobalt and Lead or their mixtures and additives are charged onto the melt, oxidizing and reducing gases are blown into the melt, the non-ferrous metal-rich phase and a non-ferrous metal-poor slag phase are discharged at the opposite end of the reactor and the phases in countercurrent to one another in essentially continuously layered form Streams flow to the outlet ends, at least a portion of the oxygen is blown into the melt from below through a plurality of independently controlled nozzles distributed across the length of the oxidation zone of the reactor, the solid feed through a plurality of independently fed expensive and gradually fed into the reactor over a considerable length of the reactor, the gradient of melt oxygen activity is adjusted by choosing the local
  • DE-B-24 17 978 describes a method according to the introduction.
  • the gas atmosphere in the reactor is conducted in cocurrent to the direction of flow of the slag phase and the exhaust gas is discharged from the reactor at the outlet end of the non-ferrous slag phase.
  • the process is also carried out autogenously.
  • the invention has for its object to reduce the metal content of the slag phase even further, to improve the heat utilization in the reactor and to enable additional heating.
  • the object is achieved according to the invention in that the gas atmosphere in the reactor is conducted in countercurrent to the flow direction of the slag phase and the exhaust gas is withdrawn from the reactor at the outlet end of the non-ferrous metal-rich phase.
  • the waste gases can be discharged upwards or to the side both through the end face of the reactor and near the end face.
  • the process is controlled with respect to the control of the gradient of the oxygen activity and the temperature in the melt as described in DE-B-24 17 978.
  • the oxygen potential in the gas atmosphere is changed by the countercurrent flow of the slag phase and the gas atmosphere, the oxygen potential and the SO 2 content being considerably reduced, in particular via the reduction zone.
  • the nozzles can be arranged side by side in several rows, so that the entire width of the melt is well gasified without the reactor having to be pivoted back and forth about its longitudinal axis.
  • a preferred embodiment is that fuels are blown into the melt at least in the reduction zone, the oxygen partial pressure in the gas atmosphere above the reduction zone is kept below 10- 3 bar, preferably below 10- 8 bar, and no SO 2 as protective gas in the reduction zone is blown in.
  • the fuel can be liquid, gaseous or solid. Its combustion is controlled so that on the one hand the required heat is generated and on the other hand the required reduction conditions in the melt and in the gas phase are maintained.
  • the protective gas for the nozzles can be hydrocarbons, which are then used as fuel, or inert gases, such as nitrogen. In the oxidation zone, as described in DE-B-24 17 978, S0 2 can be used as a protective gas.
  • a preferred embodiment is that a calming zone is connected between the reduction zone and the oxidation zone, into which no gas is blown into the melt. This achieves a good separation of the gas atmosphere in the reduction zone and the oxidation zone, individual temperature control is possible in both stages, and the sulfide-rich metal phase is separated from the metal-rich slag phase in the calming zone, as a result of which a low sulfide activity is achieved in the reduction zone.
  • a preferred embodiment is that when processing sulfidic lead or antimony concentrates, the lead or antimony sulfide contained in the fly dust in the exhaust pipe and / or exhaust gas cooling by admixing oxygen-containing gases at temperatures of 950 to 450 ° C predominantly to lead sulfate or antimony oxide and Antimony sulfate is oxidized, and the separated fly dust is mixed with the lead or antimony concentrate in an amount of 10 to 30% by weight, based on the use, and possibly with the addition of other metal sulfate-containing substances.
  • the admixture of the oxidized flue dust causes a reaction with the sulfidic concentrates even at relatively low temperatures, without additional oxygen having to be added. The rapid turnover reduces the evaporation losses of metals. Close contact of the feed components is important.
  • a preferred embodiment is that the concentrates and any additives are compacted before use in the reactor.
  • the contact of the concentrates with the additives such as lime, Si0 2 , iron oxide, recycled flying dust and possibly other metal sulfate-containing substances and carbon, is particularly close.
  • the compacting can take place, for example, by rolling, pelleting or pressing.
  • the moist, compacted particles quickly fall through the gas atmosphere and the reaction takes place in the melt. The temperature rises slowly due to the moisture of the particles, so that the evaporation losses are kept low.
  • the invention is explained in more detail and, for example, with reference to the figure and examples.
  • the figure shows schematically a cross section through a reactor.
  • the reactor 1 has the shape of a long furnace with a rounded cross section.
  • the slag drain 2 is arranged in the left end face and the rack 3 for the non-ferrous metal-rich phase is arranged near the right end face.
  • In the left end face there is an opening 4 which can be used as a work door or in which a burner can be arranged.
  • the gas outlet opening 5, which opens into the exhaust gas duct 6, and an emergency tapping 7 are arranged in the right end side.
  • the reactor 1 is divided into the working zone A, reduction zone R, calming zone B, oxidation zone O and quiet zone M, the transitions not being sharply delimited but are fluent.
  • Charging openings 8 and nozzles 9 are arranged in the oxidation zone O, only a few of which are shown schematically.
  • Nozzles 10 are also arranged in the reduction zone R, only a few of which are shown schematically.
  • the reactor 1 is mounted on races 11 and can be rotated for maintenance.
  • Lead concentrates were processed in a test reactor 4.8 m long and 1.8 m in diameter (external dimensions).
  • the limited length of the reactor does not allow continuous operation with counter-current of lead, slag and exhaust gas. Therefore, the two most important process steps were carried out: 1) partial oxidation of the concentrate mixed with aggregates and fly dust to pelletized lead and a PbO-rich slag by blowing oxygen into the melt and 2) reduction of the PbO of the slag by introducing reducing agents in succession .
  • the advantages of the invention are that the metal content of the slag phase is substantially reduced by controlling the composition of the gas phase and the temperature in the reduction zone and sulfidation of the resulting metals is prevented.
  • metals whose sulfides have low volatility it is also imperative to maintain a low oxygen potential in the reduction zone, but it can be advantageous to set such a high S0 2 partial pressure that metal sulfides are formed during the reduction, which are considerable have lower solubility in the slag than metals.
  • the heat utilization is significantly improved because the heat content of the gases from the reduction zone, which must be as high as possible for metallurgical reasons and in which an excess of reducing agent must be offered, can be largely utilized in the oxidation zone. It is possible, particularly with low-sulfur and low-iron concentrates, to introduce the necessary heat in an economical manner without disturbing the low oxygen potential required for the reduction.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)
EP79200059A 1978-02-24 1979-02-05 Verfahren zur kontinuierlichen Konvertierung von NE-Metallsulfidkonzentraten Expired EP0003853B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19782807964 DE2807964A1 (de) 1978-02-24 1978-02-24 Verfahren zur kontinuierlichen konvertierung von ne-metallsulfidkonzentraten
DE2807964 1978-02-24

Publications (2)

Publication Number Publication Date
EP0003853A1 EP0003853A1 (de) 1979-09-05
EP0003853B1 true EP0003853B1 (de) 1981-11-11

Family

ID=6032836

Family Applications (1)

Application Number Title Priority Date Filing Date
EP79200059A Expired EP0003853B1 (de) 1978-02-24 1979-02-05 Verfahren zur kontinuierlichen Konvertierung von NE-Metallsulfidkonzentraten

Country Status (15)

Country Link
US (1) US4266971A (fi)
EP (1) EP0003853B1 (fi)
JP (1) JPS54132406A (fi)
AU (1) AU523949B2 (fi)
BR (1) BR7901063A (fi)
CA (1) CA1119417A (fi)
DE (2) DE2807964A1 (fi)
ES (1) ES477955A1 (fi)
FI (1) FI68658C (fi)
MX (1) MX152092A (fi)
PH (1) PH15059A (fi)
PL (1) PL114376B2 (fi)
YU (1) YU23279A (fi)
ZA (1) ZA79115B (fi)
ZM (1) ZM1279A1 (fi)

Families Citing this family (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA1151430A (en) * 1980-02-28 1983-08-09 Charles E. O'neill Reduction smelting process
DE3029682A1 (de) * 1980-08-06 1982-03-11 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zum kontinuierlichen direkten schmelzen von metallischem blei aus sulfidischen bleikonzentraten
DE3029741A1 (de) * 1980-08-06 1982-04-01 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zum kontinuierlichen direkten schmelzen von metallischem blei aus schwefelhaltigen bleimaterialien
SE444578B (sv) * 1980-12-01 1986-04-21 Boliden Ab Forfarande for utvinning av metallinnehall ur komplexa sulfidiska metallravaror
US4514222A (en) * 1981-11-26 1985-04-30 Mount Isa Mines Limited High intensity lead smelting process
FI69871C (fi) * 1984-07-18 1986-05-26 Outokumpu Oy Foerfarande och anordning foer behandling av sulfidkoncentrat eller -malmer till raometaller
GB2173820B (en) * 1985-04-03 1989-06-28 Cra Services Smelting process
AU583906B2 (en) * 1985-04-03 1989-05-11 Cra Services Limited Smelting process
US4741770A (en) * 1985-04-03 1988-05-03 Cra Services Limited Zinc smelting process using oxidation zone and reduction zone
DE3701846A1 (de) * 1987-01-23 1988-08-04 Metallgesellschaft Ag Direktes schmelzverfahren fuer sulfidische erze
DE4108687A1 (de) * 1991-03-16 1992-11-05 Metallgesellschaft Ag Verfahren zur reduktion von ne-metalloxiden in schlacken
US5722929A (en) * 1994-08-26 1998-03-03 Southwind Enterprises Inc. Particle agglomeration with acidic sulphate
US5516976A (en) * 1994-08-26 1996-05-14 Southwind Enterprises Inc. Sulphate agglomeration
US6270554B1 (en) * 2000-03-14 2001-08-07 Inco Limited Continuous nickel matte converter for production of low iron containing nickel-rich matte with improved cobalt recovery
CN102011014B (zh) * 2010-11-21 2012-11-14 中国恩菲工程技术有限公司 连续炼铅装置及连续炼铅工艺
CN109385521B (zh) * 2018-12-21 2021-04-13 河池市生富冶炼有限责任公司 一种铅锑混合矿富氧熔池低温氧化熔炼的生产工艺
CN114657391B (zh) * 2022-03-25 2022-12-06 西安交通大学 一种无碳化铅冶金装置及冶金方法

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE495631A (fi) * 1949-05-13
US3460817A (en) * 1963-09-30 1969-08-12 Geoffrey Joynt Brittingham Furnace for continuous treatment of sulphide copper ores
US3437475A (en) * 1964-11-23 1969-04-08 Noranda Mines Ltd Process for the continuous smelting and converting of copper concentrates to metallic copper
CA893624A (en) * 1969-10-27 1972-02-22 J. Themelis Nickolas Direct process for smelting of lead sulphide concentrates to lead
CA931358A (en) * 1971-02-01 1973-08-07 J. Themelis Nickolas Process for continuous smelting and converting of copper concentrates
DE2146434A1 (de) * 1971-09-16 1973-03-22 Conzinc Riotinto Ltd Verfahren und vorrichtung zum schmelzen und/oder raffinieren von metallen
JPS5143015B2 (fi) * 1972-05-04 1976-11-19
US3941587A (en) * 1973-05-03 1976-03-02 Q-S Oxygen Processes, Inc. Metallurgical process using oxygen

Also Published As

Publication number Publication date
FI68658C (fi) 1985-10-10
BR7901063A (pt) 1979-10-02
US4266971A (en) 1981-05-12
YU23279A (en) 1982-08-31
PL213586A2 (fi) 1979-11-05
ZA79115B (en) 1979-12-27
AU4449479A (en) 1979-08-30
JPS624456B2 (fi) 1987-01-30
DE2961288D1 (en) 1982-01-14
ES477955A1 (es) 1979-07-01
MX152092A (es) 1985-05-29
PH15059A (en) 1982-06-03
CA1119417A (en) 1982-03-09
EP0003853A1 (de) 1979-09-05
ZM1279A1 (en) 1980-03-21
DE2807964A1 (de) 1979-08-30
FI68658B (fi) 1985-06-28
PL114376B2 (en) 1981-01-31
FI790389A (fi) 1979-08-25
JPS54132406A (en) 1979-10-15
AU523949B2 (en) 1982-08-26

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